Catalytic cracking process

Claim 2

In a process for the fluid catalytic cracking of a hydrocarbon oil in the absence of added hydrogen to produce products boiling in the gasoline and the fuel oil range, said process comprising contacting said hydrocarbon oil with a regenerated, porous acidic solid catalyst in a cracking vessel under conditions effective to convert said oil to said products and deposit coke on said catalyst; transferring said coked catalyst to a regeneration vessel wherein in a dense fluid bed of catalyst is maintained at an elevated temperature and burning at least a portion of said coke in the presence of an oxygen containing gas with production of carbon dioxide and carbon monoxide in said dense bed, said production being characterized by a CO 2 /CO ratio; and recycling regenerated catalyst from said regeneration vessel to said cracking vessel to catalyze further cracking and supply at least part of the heat required for said cracking, the improvement in control of said regenerator which comprises: selecting a temperature within the range of about 1200° to about 1350° F. for operation of said dense bed; adding to said circulating catalyst a metal promoter selected from the group consisting of Pt, Pd, Rh, Ir, Os and Re in an amount effective to produce a CO 2 /CO ratio within the range of 1 to 6; determining the deviation of the temperature of the dense bed with metal promoter from said selected temperature; and adjusting the flow rate of the oxygen containing gas in the direction to reduce said deviation.

Claim 3

The process claimed in claim 1 wherein said metal promoter comprises platinum.

Claim 4

The process claimed in claim 1 or 2 wherein the amount of promoter metal added is effective to produce a CO 2 /CO ratio within the range of 2 to 5.

Claim 5

In a process for the fluid catalytic cracking of a particular hydrocarbon oil in the absence of added hydrogen to produce products boiling in the gasoline and the fuel oil range, said process comprising contacting said hydrocarbon oil with a regenerated, particular porous acidic solid catalyst in a cracking vessel under conditions to convert said oil to lower molecular weight products, deposit coke on said catalyst, and deactivate said catalyst; transferring said deactivated catalyst to a regeneration vessel wherein a dense fluid bed of catalyst is maintained; burning at least a portion of said coke in the presence of an oxygen containing gas with production of carbon dioxide and carbon monoxide in said dense bed, said production being characterized by a CO 2 /CO ratio; and recycling hot regenerated catalyst from said regeneration vessel to said cracking vessel to catalyze further cracking and supply at least part of the heat required for said cracking; the improvement which comprises: selecting a product to be maximized from the group of products consisting of gasoline, fuel oil, total cracked product, and a combination of these in predetermined proportions; computing a set of operating conditions which maximize said selected product for said particular hydrocarbon oil to be cracked with said particular catalyst from a simulation of said process in which the CO 2 /CO ratio in said dense bed is allowed to vary from about 1.5 to about 100 or more, said operating conditions comprising reactor top temperature, hydrocarbon oil preheat temperature, air flow rate and CO 2 /CO ratio in said dense bed; and conducting said fluid catalytic cracking process in accordance with said computed set of values and with a catalyst inventory that contains Pt, Pd, Ph, Ir, Os or Re metal promoter in an amount sufficient to produce said calculated CO 2 /CO ratio.

Claim 6

In a process for the fluid catalytic cracking of a particular hydrocarbon oil in the absence of added hydrogen to produce products boiling in the gasoline and the fuel oil range, said process comprising contacting said hydrocarbon oil with a regenerated, particular porous acidic solid catalyst in a cracking vessel under conditions to convert said oil to lower molecular weight products, deposit coke on said catalyst, and deactivate said catalyst; transferring said deactivated catalyst to a regeneration vessel wherein a dense fluid bed of catalyst is maintained; burning at least a portion of said coke in the presence of an oxygen containing gas with production of carbon dioxide and carbon monoxide in said dense bed, said production being characterized by a CO 2 /CO ratio; and recycling hot regenerated catalyst from said regeneration vessel to said cracking vessel to catalyze further cracking and supply at least part of the heat required for said cracking; the improvement which comprises: selecting a product to be maximized from the group of products consisting of gasoline, fuel oil, total cracked product, and a combination of these in predetermined proportions; computing a set of operating conditions which maximize said selected product for said particular hydrocarbon oil to be cracked with said particular catalyst from a simulation of said process in which the CO 2 /CO ratio in said dense bed is allowed to vary from about 1.5 to about 100 or more, said operating conditions comprising reactor top temperature, hydrocarbon oil preheat temperature, air flow rate and CO 2 /CO ratio in said dense bed; and conducting said fluid catalytic cracking process in accordance with said computed set of values and with a catalyst inventory that contains Pt, Pd, Ph, Ir, Os or Re metal promoter in an amount sufficient to produce said calculated CO 2 /CO ratio.

Claim 7

The process described in claim 4 wherein said simulation comprises a kinetic predictive model of said conversion.

Claim 8

The process described in claim 5 wherein said porous, acid solid catalyst comprises a crystalline aluminosilicate zeolite having a pore size greater than about 6 Angstroms in diameter, and said metal promoter comprises platinum.

Claim 9

The process described in claim 5 wherein said set of values is computed from a simulation of said process in which the CO 2 /CO ratio in said dense bed is allowed to vary from about 1.5 to about 10.

Claim 10

The process described in claim 5 including the final step of adjusting one or more of said computed values by an EVOP procedure.

Claim 11

The process described in claim 4 wherein said computation of operating conditions is made with said CO 2 /CO ratio in said dense bed set at a value within the range of 2 to 5, and wherein the temperature of said dense bed is controlled by varying the flow rate of said oxygen containing gas.

Claim 12

The process described in claim 9 wherein said simulation comprises a kinetic predictive model of said process.

Claim 13

The process described in claim 10 wherein said porous, acid solid catalyst comprises a crystalline alumino-silicate zeolite having a pore size greater than about 6 Angstroms in diameter, and said metal promoter comprises platinum.

Claim 14

The process described in claim 9 or 10 or 11 including the final step of adjusting one or more said computed values by an EVOP procedure.